CN104342212A - Hydropyrolysis and gasification coupling method for powdered coal fluidized bed - Google Patents
Hydropyrolysis and gasification coupling method for powdered coal fluidized bed Download PDFInfo
- Publication number
- CN104342212A CN104342212A CN201310331116.9A CN201310331116A CN104342212A CN 104342212 A CN104342212 A CN 104342212A CN 201310331116 A CN201310331116 A CN 201310331116A CN 104342212 A CN104342212 A CN 104342212A
- Authority
- CN
- China
- Prior art keywords
- hydropyrolysis
- semicoke
- gas
- gasification
- hydrogen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0943—Coke
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Combustion & Propulsion (AREA)
- Industrial Gases (AREA)
Abstract
A hydropyrolysis and gasification coupling method for a powdered coal fluidized bed is disclosed. According to the method, in a first step, a heat source of a hydropyrolysis furnace of the powdered coal fluidized bed is synthesis gas from a gasification furnace, a hydrogen source comprises following two parts: (1) hydrogen in the synthesis gas and (2) hydrogen prepared by purification of gas produced in a system; in a second step, most of solid semicoke produced by hydropyrolysis is directly fed into a semicoke hopper through a coke guiding pipe, and a small part of the semicoke with a small particle size is fed into a cyclone separator together with pyrolysis gas, the semicoke enters the semicoke hopper after separation by the cyclone separator; and in a third step, a raw material of the gasification furnace is the semicoke prepared by the hydropyrolysis, the semicoke and a gasifying agent are subjected to a gasification reaction according to a certain ratio in a gasification reactor to produce high-temperature synthesis gas, and the high-temperature synthesis gas is adopted as the heat source and the hydrogen source of the hydropyrolysis furnace of the powdered coal fluidized bed. Quality of tar obtained by hydropyrolysis of coal is good. The content of obtained effective gas is high.
Description
Technical field
The present invention relates to a kind of coupling process, particularly relate to a kind of PC-FB hydropyrolysis and gasification coupling method.
Background technology
At present, domestic colliery generally adopts machine to mine, and in extraction coal, fine coal ratio accounts for 40% ~ 45%, how to utilize in this part coal become restriction Development of Coal Chemical Industry bottleneck, directly utilize fine coal generate electricity not only serious contaminate environment and also coal utilization efficiency low; Fine coal direct gasification, in coal, the material of high added value is not suggested, and is unfavorable for the comprehensive utilization of coal resources; The tar that traditional pyrolysis of coal method obtains not only yields poorly, and heavy components content is high, is unfavorable for the following process of tar, and the price of coke breeze is low simultaneously, and later use is also more difficult.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of PC-FB hydropyrolysis and gasification coupling method, and adopt the tar quality better that coal hydrogenation pyrolysis obtains, tar content is many; Coke breeze gasification can improve the utilising efficiency of coke breeze, and the effective Gas content obtained is higher.
The present invention solves above-mentioned technical problem by following technical proposals: a kind of PC-FB hydropyrolysis and gasification coupling method, is characterized in that, described PC-FB hydropyrolysis and gasification coupling method comprise the following steps:
Step one, the thermal source of PC-FB hydropyrolysis stove is the synthetic gas from vapourizing furnace, and hydrogen source is made up of two portions: a part is the hydrogen in synthetic gas; Another part is that the gas of system generation is through obtained hydrogen of purifying;
Step 2, the solid semicoke major part that hydropyrolysis generates directly enters semicoke hopper by coke guidance tube, and the semicoke that small portion granularity is little enters cyclonic separator together with pyrolysis gas, obtains semicoke and also enter in semicoke hopper after cyclonic separator is separated;
Step 3, the raw material of vapourizing furnace is the gained semicoke from hydropyrolysis, and semicoke and vaporized chemical carry out gasification reaction by a certain percentage in gasifying reactor, generates the synthetic gas of high temperature, and high-temperature synthesis gas is as the thermal source of fluidized-bed hydrogenation pyrolysis oven and hydrogen source.
Preferably, described thermal source is the high-temperature synthesis gas from gasifying section; After high-temperature synthesis gas generates in vapourizing furnace, direct entering bottom pyrolysis oven in hydropyrolysis stove carries out heat exchange with raw material fine coal and hydropyrolysis reacts, gas-phase product (tar and pyrolysis gas) and the less coke breeze of particle diameter of hydropyrolysis reaction are also taken out of from vapourizing furnace top by synthetic gas, the heat of synthetic gas is fully utilized, and does not need extra heat supply in hydropyrolysis stove simultaneously.
Preferably, described PC-FB hydropyrolysis and gasification coupling method further comprising the steps of:
Step 4, the raw material that fluidized-bed gasification furnace adopts is not the coal of traditional coal chemical industry, but the coke breeze that the reaction of fine coal hydropyrolysis generates, the pollutants such as N and S contained in coke breeze are less, can improve the work-ing life of gasifying section equipment;
Step 5, vapourizing furnace inside is the vaporizer with refractory lining, and furnace interior structure is simple, and vaporized chemical divides two-way to enter in vapourizing furnace from the upper and lower of raw material semicoke entrance from nozzle respectively by a certain percentage.
Positive progressive effect of the present invention is: the present invention adopts hydropyrolysis, and the coal tar output of acquisition is high, and light component content in tar is high; The calorific value of the coal gas obtained is about 3000Kcal/Nm3, and effective constituent (CO+H2) content in coal gas is about 6% ~ 12% more than 70%, CH4 content, and the coal gas obtained can have certain pressure, is conducive to the development of the downstream processes such as gas generation chemical.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of the hardware that PC-FB hydropyrolysis of the present invention and gasification coupling method adopt.
Embodiment
Present pre-ferred embodiments is provided, to describe technical scheme of the present invention in detail below in conjunction with accompanying drawing.
As shown in Figure 1, PC-FB hydropyrolysis of the present invention and gasification coupling method comprise the following steps:
Step one, the thermal source of PC-FB hydropyrolysis stove is the synthetic gas from vapourizing furnace, and hydrogen source is made up of two portions: a part is the hydrogen in synthetic gas; Another part is that the gas of system generation is through obtained hydrogen of purifying; Thermal source is the high-temperature synthesis gas from gasifying section.After high-temperature synthesis gas generates in vapourizing furnace, direct entering bottom pyrolysis oven in hydropyrolysis stove carries out heat exchange with raw material fine coal and hydropyrolysis reacts, gas-phase product (tar and pyrolysis gas) and the less coke breeze of particle diameter of hydropyrolysis reaction are also taken out of from vapourizing furnace top by synthetic gas, the heat of synthetic gas is fully utilized, and does not need extra heat supply in hydropyrolysis stove simultaneously.
Step 2, the solid semicoke major part that hydropyrolysis generates directly enters semicoke hopper by coke guidance tube, the semicoke that small portion granularity is little enters cyclonic separator together with pyrolysis gas (comprising the synthetic gas of gasifying section), obtains semicoke and also enter in semicoke hopper after cyclonic separator is separated;
Step 3, the raw material of vapourizing furnace is the gained semicoke from hydropyrolysis, and semicoke and vaporized chemical carry out gasification reaction by a certain percentage in gasifying reactor, generates the synthetic gas of high temperature, and high-temperature synthesis gas is as the thermal source of fluidized-bed hydrogenation pyrolysis oven and hydrogen source.
PC-FB hydropyrolysis of the present invention and gasification coupling method further comprising the steps of:
Step 4, the raw material that fluidized-bed gasification furnace adopts is not the coal of traditional coal chemical industry, but the coke breeze that the reaction of fine coal hydropyrolysis generates, the pollutants such as N and S contained in coke breeze are less, can improve the work-ing life of gasifying section equipment;
Step 5, vapourizing furnace inside is the vaporizer with refractory lining, and furnace interior structure is simple, and vaporized chemical divides two-way to enter in vapourizing furnace from the upper and lower of raw material semicoke entrance from nozzle respectively by a certain percentage.
The present invention is primarily of fluidized-bed hydrogenation pyrolytic process and gasifying process two portions composition, the process of fluidized-bed hydrogenation pyrolytic process is as follows: the fine coal A1 in coal-storage pot E6 sends in fluidized bed pyrolysis stove E4 under the effect of gas G6 together with gas G6, also the form of spiral blanking can be adopted to send in pyrolysis oven by fine coal A1 simultaneously, in fluidized bed pyrolysis stove E4, pyrolytic reaction is carried out with the vapourizing furnace E1 gained high-temperature synthesis gas G2 that gasifies, the solid semicoke A2 of pyrolysis gained enters in semicoke hopper E3 by coke guidance tube, other products G3 except semicoke A2 directly enters in cyclonic separator E2, thin burnt A3 is separated and is delivered in semicoke hopper E3.Pyrogenous origin pyrolysis gas G4(comprises the component such as synthetic gas and tar) enter in gas-liquid separator E5, tar P1 derived from the bottom of gas-liquid separator E5 and enters the deep processing of tar and refining downstream process such as grade, removing other gaseous fractions of tar P1 directly as the unstripped gas in Coal Chemical Industry downstream.
The process of gasifying process is as follows: the raw material of vapourizing furnace E1 is the semicoke A2 of pyrolysis oven and the mixture A4 of thin burnt A3, semicoke mixture A4 adopts the mode of helical feed or two-phase transportation to send in vapourizing furnace E1 from semicoke hopper, contact generating gasification with vaporized chemical G1 to react, in vapourizing furnace E1, the residue of gasification reaction is discharged through ash discharge lock hopper.What high-temperature synthesis gas G2 gasification generated does not need to carry out cooling process, is directly delivered in pyrolysis oven E4 by pipeline, does fluidizing medium and hydrogen source use.
The overall energy utilization rate of joint process is high, and in the gaseous product obtained, the content of effective gas is high, and the temperature of pyrolysis of coal process is lower, is conducive to the generation of methane, and therefore, in gaseous product, the content of CH4 wants high compared with the content that coal gasification reaction generates; Carry out pyrolytic reaction in a hydrogen atmosphere, coal tar productive rate improves greatly.
The operating parameterss such as the temperature and pressure of integrated artistic are adjustable, the service temperature of hydropyrolysis stove 400 ~ 900 DEG C, pressure 0.1 ~ 4.5MPa or atmospheric operation, the service temperature of vapourizing furnace 700 ~ 1600 DEG C, pressure 0.1 ~ 9MPa or atmospheric operation, Suitability of Coals is wider, and device amplifying power is stronger.
The fine coal that raw material granularity is less than 6mm is sent in hydropyrolysis stove by feeding machine and is mixed with high-temperature gasification synthetic gas and circulation high concentration of hydrogen or pure hydrogen, carry out hydropyrolysis reaction, generate gas-liquid-solid three kinds of products, hydropyrolysis produces the technique that most of gaseous product (comprising gasification synthesis gas) and whole tar enters downstream and processes; Portion gas product obtains high concentration of hydrogen or pure hydrogen, as hydrogen source in hydrogen recycle to pyrolysis oven after being separated; The semicoke of hydropyrolysis is all delivered in vapourizing furnace and carries out gasification reaction.In vapourizing furnace, raw material semicoke and a certain proportion of vaporized chemical (oxygen and water vapour) carry out gasification reaction, and the high-temperature synthesis gas obtained directly enters in pyrolysis oven to be made thermal source and fluidizing medium and feed coal and hydrogen and carry out hydropyrolysis reaction.The material of coal hydrogenation pyrolysis and char Gasification is carried out internal recycle by this technological design device, effectively raises energy utilization rate, and obtain the many and quality better of the tar content of high added value, in gained gas, effective gas (CO, H2 and CH4) content is high.
Those skilled in the art can carry out various remodeling and change to the present invention.Therefore, present invention covers the various remodeling in the scope falling into appending claims and equivalent thereof and change.
Claims (3)
1. PC-FB hydropyrolysis and a gasification coupling method, is characterized in that, described PC-FB hydropyrolysis and gasification coupling method comprise the following steps:
Step one, the thermal source of PC-FB hydropyrolysis stove is the synthetic gas from vapourizing furnace, and hydrogen source is made up of two portions: a part is the hydrogen in synthetic gas; Another part is that the gas of system generation is through obtained hydrogen of purifying;
Step 2, the solid semicoke major part that hydropyrolysis generates directly enters semicoke hopper by coke guidance tube, and the semicoke that small portion granularity is little enters cyclonic separator together with pyrolysis gas, obtains semicoke and also enter in semicoke hopper after cyclonic separator is separated;
Step 3, the raw material of vapourizing furnace is the gained semicoke from hydropyrolysis, and semicoke and vaporized chemical carry out gasification reaction by a certain percentage in gasifying reactor, generates the synthetic gas of high temperature, and high-temperature synthesis gas is as the thermal source of fluidized-bed hydrogenation pyrolysis oven and hydrogen source.
2. PC-FB hydropyrolysis according to claim 1 and gasification coupling method, is characterized in that, described thermal source is the high-temperature synthesis gas from gasifying section; After high-temperature synthesis gas generates in vapourizing furnace, direct entering bottom pyrolysis oven in hydropyrolysis stove carries out heat exchange with raw material fine coal and hydropyrolysis reacts, gas-phase product and the less coke breeze of particle diameter of hydropyrolysis reaction are also taken out of from vapourizing furnace top by synthetic gas, the heat of synthetic gas is fully utilized, and does not need extra heat supply in hydropyrolysis stove simultaneously.
3. PC-FB hydropyrolysis according to claim 1 and gasification coupling method, is characterized in that, described PC-FB hydropyrolysis and gasification coupling method further comprising the steps of:
Step 4, the raw material that fluidized-bed gasification furnace adopts is not the coal of traditional coal chemical industry, but the coke breeze that the reaction of fine coal hydropyrolysis generates, the pollutants such as N and S contained in coke breeze are less, can improve the work-ing life of gasifying section equipment;
Step 5, vapourizing furnace inside is the vaporizer with refractory lining, and furnace interior structure is simple, and vaporized chemical divides two-way to enter in vapourizing furnace from the upper and lower of raw material semicoke entrance from nozzle respectively by a certain percentage.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310331116.9A CN104342212B (en) | 2013-08-01 | 2013-08-01 | PC-FB hydropyrolysis and gasification coupling method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310331116.9A CN104342212B (en) | 2013-08-01 | 2013-08-01 | PC-FB hydropyrolysis and gasification coupling method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104342212A true CN104342212A (en) | 2015-02-11 |
| CN104342212B CN104342212B (en) | 2017-12-15 |
Family
ID=52498679
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310331116.9A Active CN104342212B (en) | 2013-08-01 | 2013-08-01 | PC-FB hydropyrolysis and gasification coupling method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104342212B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105062526A (en) * | 2015-08-05 | 2015-11-18 | 航天长征化学工程股份有限公司 | Coal pyrolysis gasification poly-generation system and pyrolysis gasification method thereof |
| CN105087078A (en) * | 2015-09-08 | 2015-11-25 | 航天长征化学工程股份有限公司 | Indirect pyrolysis system and pyrolysis method thereof |
| CN107083249A (en) * | 2017-05-05 | 2017-08-22 | 华东理工大学 | A kind of fine coal prepares air flow bed pyrolysis oven, the system and method vented one's spleen rich in methane thermal |
| CN107090315A (en) * | 2017-05-26 | 2017-08-25 | 上海锅炉厂有限公司 | A kind of biomass double bed gasification and pyrolysis coupled electricity-generation system and method |
| CN107541300A (en) * | 2017-10-20 | 2018-01-05 | 北京神雾电力科技有限公司 | A kind of coal grading conversion system and coal grading method for transformation |
| CN107723031A (en) * | 2017-11-23 | 2018-02-23 | 航天长征化学工程股份有限公司 | High-pressure gasification and pyrolysis integrated device for pulverized coal |
| CN109054901A (en) * | 2018-08-01 | 2018-12-21 | 万华化学集团股份有限公司 | A kind of down-flow fluidized bed using ECT-fluidized bed tandem gasification process and device |
| CN110373231A (en) * | 2019-08-16 | 2019-10-25 | 陕西延长石油（集团）有限责任公司 | The double-fluidized-bed double particles weight inferior fuels cracking gasification installations of one kind and method |
| CN110713844A (en) * | 2019-10-17 | 2020-01-21 | 中国科学院山西煤炭化学研究所 | Method for co-producing methane and light liquid tar by catalytic hydro-gasification two-step method |
| CN110846079A (en) * | 2019-11-20 | 2020-02-28 | 西安交通大学 | Solar-driven lignite poly-generation upgrading system and operation method |
| CN114763497A (en) * | 2021-01-11 | 2022-07-19 | 中国石油化工股份有限公司 | Biomass hydropyrolysis-gasification co-production process and system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03237194A (en) * | 1990-02-14 | 1991-10-23 | Yoneichi Ikeda | Decomposition and gasification of coal |
| CN101538473A (en) * | 2009-04-01 | 2009-09-23 | 上海胜帮煤化工技术有限公司 | Incoherence or weak caking coal deep processing method |
| CN102061182A (en) * | 2011-01-19 | 2011-05-18 | 吴道洪 | Method for coal hydrogenation pyrolysis and gasification coupling |
| CN102433166A (en) * | 2011-10-25 | 2012-05-02 | 陕西华祥能源科技集团有限公司 | Moving bed pulverized coal pyrolysis and fluidized bed coke powder gasification coupled device and coupling method thereof |
| CN103013576A (en) * | 2012-12-10 | 2013-04-03 | 陕西华祥能源科技集团有限公司 | IGCC (Integrated Gasification Combined Cycle) poly-generation device and method based on pyrolysis and gasification of low metamorphic powdered coal |
-
2013
- 2013-08-01 CN CN201310331116.9A patent/CN104342212B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03237194A (en) * | 1990-02-14 | 1991-10-23 | Yoneichi Ikeda | Decomposition and gasification of coal |
| CN101538473A (en) * | 2009-04-01 | 2009-09-23 | 上海胜帮煤化工技术有限公司 | Incoherence or weak caking coal deep processing method |
| CN102061182A (en) * | 2011-01-19 | 2011-05-18 | 吴道洪 | Method for coal hydrogenation pyrolysis and gasification coupling |
| CN102433166A (en) * | 2011-10-25 | 2012-05-02 | 陕西华祥能源科技集团有限公司 | Moving bed pulverized coal pyrolysis and fluidized bed coke powder gasification coupled device and coupling method thereof |
| CN103013576A (en) * | 2012-12-10 | 2013-04-03 | 陕西华祥能源科技集团有限公司 | IGCC (Integrated Gasification Combined Cycle) poly-generation device and method based on pyrolysis and gasification of low metamorphic powdered coal |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105062526A (en) * | 2015-08-05 | 2015-11-18 | 航天长征化学工程股份有限公司 | Coal pyrolysis gasification poly-generation system and pyrolysis gasification method thereof |
| CN105087078A (en) * | 2015-09-08 | 2015-11-25 | 航天长征化学工程股份有限公司 | Indirect pyrolysis system and pyrolysis method thereof |
| CN107083249A (en) * | 2017-05-05 | 2017-08-22 | 华东理工大学 | A kind of fine coal prepares air flow bed pyrolysis oven, the system and method vented one's spleen rich in methane thermal |
| CN107090315A (en) * | 2017-05-26 | 2017-08-25 | 上海锅炉厂有限公司 | A kind of biomass double bed gasification and pyrolysis coupled electricity-generation system and method |
| CN107541300A (en) * | 2017-10-20 | 2018-01-05 | 北京神雾电力科技有限公司 | A kind of coal grading conversion system and coal grading method for transformation |
| CN107723031B (en) * | 2017-11-23 | 2024-05-28 | 航天长征化学工程股份有限公司 | Pulverized coal high-pressure gasification pyrolysis integrated device |
| CN107723031A (en) * | 2017-11-23 | 2018-02-23 | 航天长征化学工程股份有限公司 | High-pressure gasification and pyrolysis integrated device for pulverized coal |
| CN109054901A (en) * | 2018-08-01 | 2018-12-21 | 万华化学集团股份有限公司 | A kind of down-flow fluidized bed using ECT-fluidized bed tandem gasification process and device |
| CN110373231B (en) * | 2019-08-16 | 2020-11-03 | 陕西延长石油（集团）有限责任公司 | Double-fluidized-bed double-particle heavy inferior fuel cracking and gasifying device and method |
| CN110373231A (en) * | 2019-08-16 | 2019-10-25 | 陕西延长石油（集团）有限责任公司 | The double-fluidized-bed double particles weight inferior fuels cracking gasification installations of one kind and method |
| CN110713844A (en) * | 2019-10-17 | 2020-01-21 | 中国科学院山西煤炭化学研究所 | Method for co-producing methane and light liquid tar by catalytic hydro-gasification two-step method |
| CN110846079A (en) * | 2019-11-20 | 2020-02-28 | 西安交通大学 | Solar-driven lignite poly-generation upgrading system and operation method |
| CN114763497A (en) * | 2021-01-11 | 2022-07-19 | 中国石油化工股份有限公司 | Biomass hydropyrolysis-gasification co-production process and system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104342212B (en) | 2017-12-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104342212B (en) | PC-FB hydropyrolysis and gasification coupling method | |
| CN101412929B (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| CN106318417B (en) | Method and system for producing biomethane and ecological methane | |
| CN101418239B (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| JP5763618B2 (en) | Two-stage dry feed gasifier and method | |
| CN101418240B (en) | High-temperature gasification process method and system for producing synthesis gas by using biomass | |
| US11220642B2 (en) | Pulverized coal gasification device and process for producing high heating value coal gas with low carbon residue content | |
| CN103045307B (en) | Pyrolysis and gasification method and device for preparing tar-free hydrogen-rich gas | |
| CN102530859A (en) | External-heating-type microwave plasma gasification furnace and synthesis gas production method | |
| CN105176594A (en) | Device and method for preparing reducing gas by lignite gasification | |
| CN104178227B (en) | A kind of fluidized bed dry distillation method and device of coal dust | |
| CN102604683A (en) | Method for co-production of synthetic gas and coal tar | |
| CN101418238B (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| US20150005399A1 (en) | Method and device for producing synthetic gas and method and device for synthesizing liquid fuel | |
| CN203360399U (en) | Fluidized bed pyrolysis and gasification coupling system for powdered coal | |
| CN205035331U (en) | Device for preparing reducing gas by lignite gasification | |
| CN100441663C (en) | Fluidization hydrogenation liquefaction method for coal | |
| CN105087078A (en) | Indirect pyrolysis system and pyrolysis method thereof | |
| CN207072928U (en) | One kind pyrolysis and gasification decoupling gasification furnace | |
| CN107723031B (en) | Pulverized coal high-pressure gasification pyrolysis integrated device | |
| CN106995728B (en) | Combined process for efficiently and cleanly preparing oil and gas products by using pulverized coal | |
| Khan et al. | Catalytic biomass gasification in decoupled dual loop gasification system over alkali-feldspar for hydrogen rich-gas production | |
| CN103484181A (en) | System and process for manufacturing substitute natural gas by utilizing coal | |
| CN110240943B (en) | Process and device for preparing synthesis gas by combined feeding | |
| Yu et al. | Experimental study on the gasification characteristics of biomass with CO2/air in an entrained-flow gasifier |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 201210 Shanghai City, Pudong New Area Chinese Shenjiang Road (Shanghai) Free Trade Zone No. 5709 Building 1 building 1008 room 10 Applicant after: SPANG TECHNOLOGY CO.,LTD. Address before: Room 11, building 68, Hua Tuo Road, Zhangjiang hi tech park, Shanghai, 201210, China Applicant before: Shanghai wins chemical technology Limited by Share Ltd. Address after: Room 11, building 68, Hua Tuo Road, Zhangjiang hi tech park, Shanghai, 201210, China Applicant after: Shanghai wins chemical technology Limited by Share Ltd. Address before: 201203 Shanghai City, Pudong New Area Road No. 68, building 11, Zhangjiang hi tech Hua Tuo Applicant before: SHCCIG (SHANGHAI) SPANG CHEMICAL TECHNOLOGY Co.,Ltd. |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |